Apparatus for leaching zinc concentrates

ABSTRACT

An apparatus for leaching zinc concentrates which comprises: a pressure vessel for charging therein a solution containing at least free sulfuric acid and iron ions, a stirrer which is disposed in the pressure vessel, an oxygen gas supply pipe that extends into the pressure vessel from the outside of the pressure vessel, the oxygen gas supply pipe having an oxygen gas inlet port which opens below the stirrer, and a discharge pipe through which an iron-containing, acidic solution or a slurry that results from the reaction of said solution containing at least free sulfuric acid and iron ions is discharged to the outside of the pressure vessel, the discharge pipe having a drain port which is open in a lower part of said pressure vessel.

CROSS REFERENCE TO RELATED APPLICATION

[0001] This application is a Divisional application of application Ser.No. 10/058,438, filed Jan. 28, 2002, the entire contents of which areincorporated by reference herein.

BACKGROUND OF THE INVENTION

[0002] 1. Field of the Invention

[0003] This Invention relates generally to a hydrometallurgical zincproduction process by which zinc and other valuable metal elements suchas lead, gold and silver, as well as the by-product elemental sulfur(which is hereunder referred to simply as “sulfur”) are recovered fromzinc concentrates which are sulfides containing not only zinc but alsoother valuable metal elements such as lead, gold and silver. Inparticular, the invention relates to the step of leaching zincconcentrates in the process.

[0004] 2. Background Information

[0005] Known prior art techniques for leaching zinc concentrates andother steps in the hydrometallurgical zinc production process aredisclosed in JP No. 2,856,933 and JP 6-43619B. In the method of treatingzinc concentrates according to JP No. 2,856,933, the leaching step iscarried out in two stages. Prior to leaching, the zinc concentrates areroasted to form calcined zinc (calcines) which are then subjected toneutral leaching. In the next stage, using the spent electrolyte (returnacid) from the electrolytic winning step, strong acid leach is effectedto dissolve the unleached zinc concentrate and the slightly soluble zincferrite which results from the roasting step. The ion of trivalent iron(sometimes called “ferric iron”) which is necessary to leach zinc is notfully supplied by the iron that occurs from the decomposition of zincferrite, so after the leaching step, the ion of divalent iron (sometimescalled “ferrous iron”) is recycled after oxidization. As the result ofperforming this leaching process for 6-10 hours at 90-95° C., a zincrecovery of about 99% can be achieved. The residues from the leachingstep are subjected to either a pyrometallurgical treatment in a blastfurnace to recover any valuable metals present or flotation toconcentrate the valuable metals for subsequent recovery.

[0006] In the method described in JP 6-43619B, the step of leaching zincconcentrates consists of at least two stages. After the zinc concentrateis pulverized into fine particles, the first stage of leaching iseffected under superatmospheric condition by applying an oxygen pressureat a temperature of 125-160° C. to give a final free sulfuric acidconcentration of 20-60 g/L and a ferric ion concentration of 1-5 g/L.This results in incomplete leaching of zinc. The second stage ofleaching is effected under atmospheric pressure using an excess amountof the spent electrolyte (return acid) generated in the electrolyticwinning step, with oxygen being supplied to give a free sulfuric acidconcentration of 60-160 g/L and a ferric ion concentration of 2-3 g/L.This yields a solution of zinc sulfate and a leach residue. Since theresidue contains the remaining part of zinc, copper and iron, as well asthe greater part of lead and noble metals, flotation is applied torecover these metal values as separate entities.

[0007] The prior art methods described above have the advantage thatthey can be incorporated into the existing circuit of roasting, leachingand electrolytic winning steps in the hydrometallurgical zinc producingprocess and that the need to reinforce the existing equipment is fairlysmall. In addition, the percent zinc recovery from the zinc concentrateis fairly high and it is also possible to recover valuable metalelements such as lead and precious metals. However, the prior artmethods have their own drawbacks. To implement the method disclosed inJP No. 2,856,933, roasting equipment, sulfuric acid recovering equipmentand even equipment for oxidizing the ion of divalent iron have to beadded, leading to a higher construction cost; in addition, it takes anunduly long time to achieve complete leaching of zinc into solution. Themethod disclosed in JP 6-43619B has the following disadvantages: thepulverizing step is necessary; the leaching step involves a multiple ofstages; the leaching temperature is so high that the operating cost isincreased; the percent zinc leach is not high enough and, what is more,the sulfur which is a by-product forming as the zinc concentrate isleached is melted in the hot leach liquor and the reaction for leachingzinc from the zinc concentrate is inhibited, thereby prolonging theleach time while contributing to a further decrease in the percent zincleach.

SUMMARY OF THE INVENTION

[0008] In order to solve these problems of the prior art, the presentinventors conducted intensive studies and found that by grinding andleaching the zinc concentrate either simultaneously or separately, theingredients that stayed on the surface of the concentrate to interferewith the leaching reaction can be effectively stripped or separated awayto achieve a marked improvement in the rate at which zinc is leached.

[0009] When oxygen was fed into the piping to pressurize its interiorwhile the leach liquor was being circulated by means of a pump, the ironion that had been consumed to the divalent form during the reaction wasregenerated to the trivalent form which could be put again into theleaching cycle, thereby successfully oxidizing the iron ion withoutusing any large-scale pressure vessel.

[0010] The present inventors also attempted the following process:oxygen was supplied in a pressurized atmosphere to oxidize a liquorcontaining both free sulfuric acid and the divalent iron ion, therebypreparing an iron-containing, acidic solution into which the zincconcentrate was subsequently charged for leaching or, alternatively, thezinc concentrate was directly leached in the pressurized atmosphere,thereby causing the oxidization of the ferrous ion in the liquor and theleaching of the zinc concentrate under superatmospheric pressure to beaccomplished in one step; thereafter, the zinc concentrate was leachedas it was ground and then it was leached with the iron-containing,acidic solution or subjected to another cycle of oxidizing and leachingsteps in the pressurized atmosphere; by means of this approach, both theleach rate and the percent leach were remarkably improved for not onlyzinc but also other valuable metals such as cadmium and copper in thezinc concentrate.

[0011] When a pressure vessel such as an autoclave having oxygen gasinlet ports, a drain port through which the iron-containing, acidicsolution or the leached slurry was to be discharged, and any othernecessary ports provided at specified sites of the vessel was used toimplement the above-described leaching method under superatmosphericpressure with oxygen gas being supplied through the oxygen gas inletports, the rate of reaction for the oxidation of the ferrous ion wassufficiently increased that not only the rate of the reaction for theleaching of the zinc concentrate but also the percent leach could beimproved to realize a substantial reduction in the scale and the cost ofthe leaching equipment.

BRIEF DESCRIPTION OF THE DRAWING

[0012]FIG. 1 is a schematic cross section of a leaching apparatus usedto oxidize the solution containing free sulfuric acid and ferrous ionsand leach the zinc concentrate, wherein reference numeral 1 designates apressure vessel, 2 an oxygen blow pipe, 3 a titanium lining, 4 a chargepipe, 5 a discharge pipe, 6 a stirrer, and 7 a partition.

DETAILED DESCRIPTION OF THE INVENTION

[0013] The present invention provides the following methods according toits first aspect:

[0014] 1. A method of leaching zinc from a zinc concentrate by grindingthe zinc concentrate in an aqueous solution containing free sulfuricacid and ferric ions.

[0015] 2. The method according to item 1, wherein said grinding iseffected at atmospheric pressure.

[0016] 3. The method according to item 1 or 2, wherein any by-productthat forms on the surfaces of the particles of said zinc concentrate asthe result of said leaching is stripped by said grinding in order toshorten the time of said leaching.

[0017] 4. The method according to any one of items 1-3, wherein oxygenis supplied into the post-leach solution containing the ferrous ionsthat result from the reduction of said ferric ions during said leaching,whereby said ferrous ions are oxidized to ferric ions and the solutioncontaining said ferric ions is returned to said grinding step.

[0018] 5. The method according to any one of items 1-3, wherein oxygenis supplied into a pipe through which said aqueous solution istransferred to said grinding step, whereby the interior of said pipe ispressurized.

[0019] 6. The method according to item 4, wherein oxygen is suppliedinto a pipe through which said post-leach solution is returned to saidgrinding step, whereby the interior of said pipe is pressurized.

[0020] 7. The method according to any one of items 1-6, wherein theconcentration of free sulfuric acid that is present in said aqueoussolution at the end of the leaching is controlled to be no less than 40g/L, thereby preventing the formation of jarosite.

[0021] 8. The method according to any of items 1-7, wherein theconcentration of ferric ions in said aqueous solution is controlled tolie within the range of 5-60 g/L.

[0022] 9. The method according to any one of items 1-8, wherein theresidue remaining after said leaching in which at least one metalelement in said zinc concentrate that is selected from among lead, goldand silver is concentrated is subjected to flotation to recover said atleast one metal element.

[0023] 10. The method according to item 9, in which the float obtainedby said flotation is heated to a temperature not lower than the meltingpoint of sulfur, whereby the elemental sulfur in said float isevaporated and recovered.

[0024] These methods according to the first aspect of the invention arespecifically implemented as described below.

[0025] Using both the spent electrolyte (return acid) with a freesulfuric acid concentration of about 150-200 g/L that results from theelectrolytic winning stage and the post-treatment solution that nolonger contains iron, temperature is raised to 80-95° C. for initiatingthe zinc leaching reaction. The reaction involved is expressed by thefollowing equation:

ZnS+Fe₂(SO₄)₃→ZnSO₄+2FeSO₄+S  (A)

[0026] The trivalent iron necessary for promoting the reaction (A) issupplied from the iron in the zinc concentrate to be treated. Duringleaching, the concentration of the ferric ion is preferably adjustedwithin the range of 5-60 g/L, more preferably in the range of 5-15 g/L.If the concentration of the ferric ion is below 5 g/L, the reaction (A)does not proceed at a satisfactorily high rate; on the other hand, theeffect of the ferric ion is saturated if its concentration exceeds 60g/L.

[0027] The reaction (A) progresses with the passage of time; on theother hand, elemental sulfur and other by-products of the reaction aredeposited on the surfaces of the particles of the zinc concentrate toreduce the surface areas available for the required reaction and, as aconsequence, the reaction rate decreases in the subsequent period andconsiderable time is required to leach all zinc that is contained.

[0028] In methods 1-10 of the invention, the zinc concentrate is leachedas it is ground by means of a grinding machine such as a ball mill inorder to strip or separate the elemental sulfur and other by-products ofthe reaction (A) from the surfaces of the particles in the concentrate.If desired, the grinding step may be performed separately from theleaching step. After being leached once, the zinc concentrate is groundto strip or separate the by-products from the surfaces of the particlesand then a second leach is performed, followed by another grindingoperation; thus, the grinding and leaching steps may alternate in arepeated manner to attain the intended object of the invention. Thegrinding machine to be used in the grinding operation is not limited toa ball mill and any type of machine can be used as long as it fits thepurpose of stripping or separating the elemental sulfur and otherby-products from the surfaces of the particles in the zinc concentrate.Other grinding machines that can be used include a rod mill, a towermill, a vibrating mill, and an attrition mill. The grinding alsocontributes to further refining the zinc concentrate and its specificsurface area is sufficiently increased to promote the leaching process.The particle size of the zinc concentrate to be ground is not limited toany particular value; however, for shorter leach times, smaller particlesizes are desirable, as exemplified by a median size of 1-100 μm and a90% particle size of 50-1,000 μm. Particles with median sizes finer than1 μm are most likely to scatter in the process of ore transfer, causinga lower yield of the raw material. If the median size is greater than100 μm, the intended effect of the grinding operation is not attained.

[0029] In the grinding process, the slurry should have higherconcentrations, preferably at least 30 g/L.

[0030] As the result of the leaching reaction, a leach residue occursbut depending on the leaching conditions, lead jarosite may also beformed. The presence of such lead jarosite increases the amount of theleach residue to be formed, hence, the cost of the residue treatment. Inorder to suppress the formation of jarosite during the leachingreaction, the concentration of free sulfuric acid present at the end ofthe leaching need be controlled at 40 g/L and more.

[0031] As is evident from the equation (A), the progress of the leachingof the zinc concentrate is accompanied by the consumption of the ferricion required to sustain the leaching process. If the ferric ion is lost,the leaching reaction (A) no longer proceeds but simply stops. In orderto prevent this trouble, the ferric ion is kept supplied in an amountcorresponding to the level of zinc in the zinc concentrate or,alternatively, the evolved ferrous ion is oxidized to regenerate theferric ion so that it is recycled to the leaching circuit. Thisoxidation reaction is represented by the following equation (B):

2FeSO₄+½O₂+H₂SO₄→Fe₂(SO₄)₃+H₂O  (B)

[0032] Under atmospheric pressure, this reaction for oxidation of theferrous ion proceeds at very slow rate. A common practice is creating asuperatmospheric condition in a pressure vessel such as an autoclave andperforming the oxidation reaction at an accelerated rate. However,pressure vessels such as an autoclave are not only difficult to handlebut also expensive. In the present invention, a pressurized state iscreated within pipes and as the solution flows through the pipes, theferrous ion is oxidized to regenerate the ferric ion which is thenreturned for further use in the leach step.

[0033] If the leaching of the zinc concentrate and the oxidizing of theferrous ion are performed in successive stages, about 95% of the zinccontent in the zinc concentrate can be leached in about 30 minutes whichis considerably shorter than the reaction time of the conventionalmethods. While this effect is attained by grinding the zinc concentratein the leaching aqueous solution, it should be remembered thatalternating the grinding and leaching steps is also effective.

[0034] The leachate from the leaching step passes through thepurification step to be transferred to the electrolytic winning step, inwhich zinc is recovered from the leachate as electrolytic zinc. Theleach residue contains lead, silver, elemental sulfur and preciousmetals other than silver and these must be separated out. To this end,the leach residue is sent to the flotation step so that sulfides andelemental sulfur are separated from the metal fraction. Stated morespecifically, solid-liquid separation is performed after the leachingstep to make a concentrated slurry of the leach residue which issubjected to flotation with air being blown into the slurry as itremains liquid. This process causes sulfur and sulfides to betransferred to the float whereas lead, silicates and precious metals aretransferred to the tailings.

[0035] The elemental sulfur in the float is evaporated at a temperaturehigher than its melting point and the resulting vapor of sulfur iscooled to condense in a recoverable form. The lead and precious metalscontained in the tailings are recovered by a pyrometallurgicaltreatment.

[0036] According to its second aspect, the present invention providesthe following methods:

[0037] 11. A method of leaching zinc concentrates which comprises thepressurized oxidation step of oxidizing a solution containing freesulfuric acid and iron ions in a pressurized oxidizing atmosphere toprepare an iron-containing, acidic solution and the grinding andleaching step of leaching zinc from a zinc concentrate as the latter isground in said iron-containing, acidic solution.

[0038] 12. A method of leaching zinc concentrates which comprises thepressurized oxidation and leaching step of oxidizing a solutioncontaining free sulfuric acid and iron ions in a pressurized oxidizingatmosphere to prepare an iron-containing, acidic solution which is usedto leach zinc from a zinc concentrate and the grinding and leaching stepof leaching zinc from the resulting slurry as the latter is ground.

[0039] 13. A method of leaching zinc concentrates which comprises thepressurized oxidation step of oxidizing a solution containing freesulfuric acid and iron ions in a pressurized oxidizing atmosphere toprepare an iron-containing, acidic solution, the leaching step ofleaching zinc from a zinc concentrate by means of said iron-containing,acidic solution, and the grinding and leaching step of leaching zincfrom the resulting slurry as the latter is ground.

[0040] 14. The method according to item 11 or 13, which further includesan additional grinding and leaching step in which zinc is leached fromthe slurry resulting from the first grinding and leaching step as thelatter is ground in said iron-containing, acidic solution.

[0041] 15. The method according to item 12, which further includes anadditional pressurized oxidation and leaching step in which the slurryfrom the first grinding and leaching step in the pressurized oxidizingatmosphere is oxidized to regenerate an iron-containing, acidic solutionwhich is used to leach zinc from said slurry.

[0042] 16. The method according to item 15, which further includes anadditional grinding and leaching step in which zinc is leached from theslurry resulting from said additional pressurized oxidation and leachingstep as the latter is ground.

[0043] 17. The method according to item 11, 13 or 14, wherein saidpressurized oxidation is performed at a solution's temperature of 90° C.or higher.

[0044] 18. The method according to item 12, 15 or 16, wherein saidpressurized oxidation and leaching step and said additional pressurizedoxidation and leaching step are performed at a solution's temperature of90-120° C.

[0045] 19. The method according to any one of items 11-18, wherein theconcentration of free sulfuric acid present in the slurry at the end ofsaid leaching is 2 g/L or more.

[0046] 20. The method according to any one of items 11-19, wherein theconcentration of ferric ions in said iron-containing, acidic solution is2 g/L or more.

[0047] According to its third aspect, the present invention provides thefollowing apparatus:

[0048] 21. An apparatus for leaching zinc concentrates which comprises apressure vessel to be charged with a solution containing at least freesulfuric acid and iron ions, oxygen gas supply pipes that extend intosaid vessel from the outside and which have oxygen gas inlet ports openbelow stirrers, and a pipe through which an iron-containing, acidicsolution or a slurry that results from the reaction of said solutioncontaining at least free sulfuric acid and iron ions is discharged tothe outside has a drain port open in the lower part of said vessel.

[0049] Methods 11-20 according to the second aspect of the invention andapparatus 21 according to its third aspect are operated in the followingmanner.

[0050] A solution containing free sulfuric acid and iron ions that hasbeen prepared using primarily the spent electrolyte (return acid) fromthe zinc electrolytic winning step which has preferably a free sulfuricacid concentration of 150-200 g/L and the zinc solution that is formedby removing iron is oxidized in a pressurized atmosphere at an elevatedtemperature which is preferably at least 90° C., more preferably in therange of 90-120° C., to make an iron-containing, acidic solution. Theiron-containing, acidic solution is used in the subsequent step ofleaching the zinc concentrate in a pressurized atmosphere or an airatmosphere. The rate of iron ion oxidation can be increased by elevatingthe temperature of the iron-containing, acidic solution in a pressurizedatmosphere to 90° C. or higher. If both oxidation of theiron-containing, acidic solution and leaching of the zinc concentrateare to be performed in the pressurized atmosphere, the temperature ofthe solution may be elevated to 90-120° C. and this contributes not onlyto increasing the rate of iron ion oxidation but also to preventing themelting of sulfur which is a by-product of the leaching of the zincconcentrate; as a result, both the percent leach of zinc from the zincconcentrate and the rate of its leach can be improved. Another advantageof selecting a leach temperature in the range of 90-120° C. is thatthere will be no re-precipitation of Fe and Cu in the solution and thepercent recovery of these metals can be increased while shortening thereaction time. As already mentioned, the reaction involved in theleaching of zinc concentrates is expressed by the following equation:

ZnS+Fe₂(SO₄)₃→ZnSO₄+2FeSO₄+S  (A)

[0051] The trivalent iron necessary for promoting the reaction (A) issupplied from the iron in the zinc concentrate to be treated. Duringleaching, the concentration of ferric ions in the iron-containing,acidic solution is adjusted to 2 g/L and above, preferably in the rangeof 2-60 g/L, more preferably in the range of 2-15 g/L. If theconcentration of ferric ions is below 2 g/L, the reaction (A) does notproceed at a satisfactorily high rate; on the other hand, if theconcentration of the ferric ion exceeds 60 g/L, the oxidizing effect issaturated and no commercial feasibility is realized. Copper, cadmium andother valuable metals in the zinc concentrate are leached in the sameway as zinc is.

[0052] The reaction (A) progresses with the passage of time; if the zincconcentrate is leached at a solution's temperature of 120° C. or below,the sulfur which forms as a by-product of the leaching reaction does notmelt but it is deposited to some extent on the surfaces of the particlesof the yet to be leached zinc concentrate to reduce the surface areasavailable for the required reaction and, as a consequence, the leachingreaction rate decreases in the subsequent period and considerable timeis required to leach all zinc that is contained in the zinc concentrate.

[0053] In order to solve this problem, it is necessary to detach orseparate the sulfur that has formed as a by-product of the reaction (A)and which has been deposited on the surfaces of the particles in thezinc concentrate. To this end, the slurry resulting from the step ofleaching the zinc concentrate is ground by means of a grinding machinesuch as a ball mill. The grinding machine to be used in the grindingoperation is not limited to a ball mill and any type of machine can beused as long as it fits the purpose of detaching or separating thesulfur from the surfaces of the particles in the zinc concentrate. Othergrinding machines that can be used include a rod mill, a tower mill, avibrating mill and an attrition mill. The grinding also contributes tofurther refining the zinc concentrate and its specific surface area issufficiently increased to promote the leaching of the slurry from thegrinding step. The particle sizes of the zinc concentrate to be groundand the slurry from the grinding step are not limited to any particularvalues; however, for shorter leach times, smaller particle sizes aredesirable, as exemplified by a median size of 1-100 μm and a 90%particle size of 50-1,000 μm. Particles with median sizes finer than 1μm are most likely to scatter in the process of transferring the zincconcentrate, causing a lower yield of the raw material. If the mediansize is greater than 100 μm, the intended effect of the leachingoperation is not attained.

[0054] As the result of the leaching reaction, a leach residue occursbut depending on the leaching conditions, lead jarosite may also beformed. The presence of such lead jarosite increases the amount of theleach residue to be formed, hence, the cost of the residue treatment. Inorder to suppress the formation of jarosite during the leachingreaction, the concentration of free sulfuric acid present at the end ofthe leaching need be controlled at 2 g/L and more, preferably at 40 g/Land more.

[0055] As is evident from the equation (A), the progress of the leachingof the zinc concentrate is accompanied by the consumption of the ferricion required to sustain the leaching process. If the ferric ion is lost,the leaching reaction (A) no longer proceeds but simply stops. In orderto prevent this trouble, the ferric ion is kept supplied in an amountcorresponding to the level of zinc in the zinc concentrate or,alternatively, the evolved ferrous ion is oxidized to regenerate theferric ion so that it is recycled to the leaching circuit. As alreadymentioned, this oxidation reaction is represented by the followingequation (B):

2FeSO₄+½O₂+H₂SO₄→Fe₂(SO₄)₃+H₂O  (B)

[0056] This reaction for oxidation of the ferrous ion can be carried outunder atmospheric pressure but the reaction rate is very slow. In thepresent invention, the iron-containing, acidic solution is prepared byoxidizing the solution that contains free sulfuric acid and iron ions ina pressurized oxidizing atmosphere. The invention is also characterizedin that depending on the case, the reaction of oxidizing the solutionand the reaction of leaching the zinc concentrate may be performed inone step in a pressurized oxidizing atmosphere.

[0057] Stated more specifically, a pressurized atmosphere created in apressure vessel such as an autoclave is supplied with an oxidizer suchas oxygen in order to raise the concentration of dissolved oxygen in thesolution containing free sulfuric acid and ferrous ions, whereby theferrous ion is oxidized to the ferric ion to prepare an iron-containing,acidic solution; if desired, the same pressurized atmosphere may furtherbe used to leach zinc from the zinc concentrate under superatmosphericcondition by means of the iron-containing, acidic solution.Alternatively, zinc may be leached from the zinc concentrate by means ofthe iron-containing, acidic solution under atmospheric condition.Blowing of oxygen gas is a typical means of oxidizing the ferrous ion inthe solution in the pressure vessel but oxygen may be supplied by addingother oxidizers.

[0058]FIG. 1 shows a preferred example of the apparatus according to thethird aspect of the invention, in which oxidation of the solutioncontaining free sulfuric acid and iron ions and leaching of the zincconcentrate by means of the resulting iron-containing, acidic solutionare performed in one step in the pressure vessel. The pressure vesselindicated by 1 is preferably lined with a titanium layer 3 in order tomake it acid resistant and to prevent deterioration with oxygen gas.Oxygen gas is used as the oxidizer and it has preferably a purity of atleast 99.5%. Oxygen gas is introduced into the solution through oxygenblow pipes 2. If the inlet ports of these pipes 2 are open understirrers 6, the oxygen gas blown into the solution is dispersed andcomminuted into finer sizes by the rotating action of the stirrers 6and, in addition, gas-liquid contact is enhanced to increase theefficiency of oxidation of the ferrous ion in the solution. The amountof oxygen supply is controlled such that the oxygen partial pressure inthe atmosphere in the pressure vessel 1 is held constant within therange of 0.7-1.0 MPa. Controlling the amount of oxygen supplycontributes to controlling the oxidation and leaching rates. If theoxygen partial pressure is 0.7 MPa or higher, the rate of oxidizing theferrous ion is increased. In order to assure the corrosion resistance ofthe pressure vessel 1 and other equipment, the oxygen partial pressureis preferably no higher than 1.0 MPa. The diameter of the oxygen blowpipes 2 depends on the amount of oxygen gas to be supplied but in orderto ensure that finer bubbles of oxygen gas will evolve in the solution,smaller diameters are preferred.

[0059] As shown in FIG. 1, partitions 7 are desirably provided withinthe pressure vessel 1 to ensure that the slurry will flow in the vesselas the reaction progresses. Alternatively, the solution may be conductedthrough a plurality of separate vessels by a suitable means such as apump. Stirrers 6 are provided in the respective compartments defined bypartitions 7. The blades of stirrers 6 are preferably of a turbine type.With turbine blades, the oxygen gas blown in through the inlet ports ofoxygen supply pipes 2 is diffused into finer bubbles and in the radialdirection of the turbine blades. As a result, none of the oxygen gassupplied will be stagnant in the vessel 1 and the rate of the reactionfor the oxidation of ferrous ions in the solution is increased. Thisimprovement in the oxidation rate allows for the provision of baffleplates on the inner surfaces of the pressure vessel 1.

[0060] Since the interior of the pressure vessel 1 is divided intocompartments by the partitions 7, the slurry of the zinc concentrate andthe solution containing free sulfuric acid and ferrous ions will betransferred from one compartment to the next. Preferably, a charge pipe4 is positioned such that the inlet port is open in the lower part ofthe first compartment, into which the slurry is charged to oxidize theferrous ion and leach the zinc concentrate in the pressurized oxidizingatmosphere; the slurry is preferably transferred to the next compartmentafter it has undergone the necessary reactions in the first compartment.The part of the slurry which has not been fully leached in the firstcompartment has high specific gravity since it contains a large amountof the unreacted zinc concentrate; hence, the slurry is better withdrawnfrom the lower part of the vessel 1 in order to achieve efficientleaching in the next leaching compartment. Withdrawing the slurry fromthe liquid surface of the solution is by no means efficient since oxygenblowing has caused many bubbles to form on the liquid surface. Theslurry that has undergone oxidation and leaching in all compartments isdrained to the outside of the vessel through a discharge pipe 5 whosedrain port is open in the lower part of the last compartment. The slurryis then subjected to grinding. The slurry obtained by the sequence ofpressurized oxidizing/leaching and grinding/leaching steps in thepressure vessel 1 may, depending on the need, be charged again into thevessel 1 and subjected to an additional pressurized oxidizing/leachingstep in a pressurized oxidizing atmosphere. Thus, by repeating the stepsof oxidation and leaching in the pressure vessel, with thegrinding/leaching step inserted between successive oxidation/leachingsteps, not only the rate of leaching the zinc concentrate but also thepercent leach can be improved significantly.

[0061] The leachate from the step of leaching zinc from the zincconcentrate passes through the purification step to be transferred tothe electrolytic winning step, in which zinc is recovered from theleachate as electrolytic zinc. The leach residue contains lead, gold,silver and other valuable metals, as well as sulfur and these must beseparated out. To this end, the leach residue is sent to the flotationstep so that sulfides and sulfur are separated from the metal fraction.Stated more specifically, solid-liquid separation is performed after theleaching step to make a concentrated slurry of the leach residue whichis subjected to flotation with air being blown into the slurry as itremains liquid. This process causes sulfur and sulfides to betransferred to the float whereas lead, silicates, gold and silver aretransferred to the tailings.

[0062] The sulfur in the float is evaporated at a temperature higherthan its melting point and the resulting vapor of sulfur is cooled tocondense in a recoverable form. The lead, gold and silver contained inthe tailings are recovered by a pyrometallurgical treatment.

[0063] If it is only oxidation of the ferrous ion in the solution thatis to be performed in the pressurized oxidizing atmosphere, only thesolution containing free sulfuric acid and ferrous ions may of course becharged into the pressure vessel 1 through the charge pipe 4 andoxidized in that vessel to make an iron-containing, acidic solution,which is eventually drained to the outside of the vessel 1 via thedischarge pipe 5 so that the zinc in the zinc concentrate is leached orboth ground and leached in air atmosphere.

[0064] The following examples are provided for further illustrating thepresent invention but they are by no means intended to limit thetechnical scope of the invention.

EXAMPLES

[0065] The invention as it relates to methods 1-10 is illustrated belowby Examples 1 and 2.

Example 1

[0066] A commercial test grinding machine of an attrition mill type,called ATTRITOR (trade name), was used as a grinding machine. TheATTRITOR had a capacity of 5.4 L (200 mm^(φ)×176 mm^(H)); it was made ofSUS 304; the motor was operating at 170 rpm and faster; the grindingmedia were alumina balls (9 mm^(φ); charged in about 3 kg).

[0067] An aqueous leaching solution was prepared by adjusting the zincconcentration to 100 g/L, the ferric ion concentration to 30 g/L and thefree sulfuric acid concentration to 40 g/L.

[0068] The zinc concentrate to be treated had the composition shown inTable 1. Metal elements such as Zn, Fe, Pb, Cd and Cu were contained assulfides in the zinc concentrate. The zinc concentrate had a mediandiameter of 25 μm and a 90% particle size of 70 μm. TABLE 1 Metalelement Zn Fe Pb Cd Cu Content (wt %) 53.67 4.80 1.26 0.26 1.51

[0069] Two liters (2.0 L) of the aqueous leaching solution was fed intothe grinding machine and heated to 90° C. Sixty grams (60 g) of the zincconcentrate was then added to the heated aqueous leaching solution andthe grinding machine was run to start grinding and leaching operations.With the slurry being sampled at intervals of 5 minutes, the grindingmachine was continuously run for 30 minutes to have the zinc concentratereact with the aqueous leaching solution in it. The collected sampleswere filtered and the cake (residue) was washed thoroughly with waterand the contents of the individual metals in the residue were comparedwith the initial contents to determine the percent zinc leach.

[0070] The results are shown in Table 2, from which one can confirm that95% zinc leach was accomplished by only 30-minute leaching. TABLE 2 Time(min) Percent zinc leach 5 40.8 15 46.6 20 70.2 25 92.7 30 95.1

Example 2

[0071] A grinding and leaching test was conducted as follows using theATTRITOR (see Example 1). A mother liquor was prepared that had a zincconcentration of 100 g/L, a ferric ion concentration of 15 g/L and afree sulfuric acid concentration of 40 g/L; a zinc concentrate of thesame composition as used in Example 1 was added to this mother liquor ata concentration of 30 g/l and leaching was performed for 10 minutes.After the leaching, the slurry was adjusted to have a concentration of200 g/L and ground with the ATTRITOR for 1 minute. After the grinding,the slurry was filtered and the residue was recovered. These stepscomprise one test run. Thereafter, the residue was put back into themother liquor and subjected to another test run. The number of test runsconducted and the percent leach in each run are shown in Table 3 below.TABLE 3 Test run Percent zinc leach First 72.7 Second 89.5 Third(consisting 96.5 of only 10-min leach)

[0072] Thus, 96.5% zinc leach was achieved by conducting two test runs,followed by 10-min leach. Inclusive of the grinding time, the totalprocessing time was only about 32 minutes and high percent zinc leachcould be realized in as short a time as in Example 1.

[0073] In methods 1-10 according to the first aspect of the invention,zinc concentrates were leached with a grinding machine such as a ballmill as elemental sulfur and other by-products were detached andseparated from the surfaces of the particles in the zinc concentrates;the leach time was only about 30 minutes which was less than a tenth ofthe heretofore required 6-10 hours. The ferric ion that was consumed byleaching could be regenerated by introducing oxygen into the piping andthis eliminated the need of providing a pressure vessel such as anautoclave. Since the overall leach time was considerably shorter thanrequired in the prior art and there was no need to provide oxidizingequipment, methods 1-10 could be combined to realize substantial cuts inconstruction and operating costs. As another advantage, these methodscan be incorporated into the existing facilities, enabling more zinc tobe produced by small addition of equipment.

[0074] Described below is Example 3 which relates to methods 1-20according to the second aspect of the invention, as well as apparatus 21according to its third aspect.

Example 3

[0075] A ball mill was used as a grinding machine. The ball mill had acapacity of 4.5 L (64 mm^(φ)×350 mm^(H)); it was made of SUS 316; themotor was operating at 55 rpm; the grinding media were alumina balls (9mm^(φ), charged in about 9.5 kg).

[0076] An iron-containing, acidic solution was prepared by adjusting thezinc concentration to 110 g/L, the ferrous ion concentration to 15 g/Land the free sulfuric acid concentration to 96 g/L.

[0077] The zinc concentrate to be treated had the composition shown inTable 4. Metal elements such as Zn, Fe, Pb, Cd and Cu were contained assulfides in the zinc concentrate. The zinc concentrate had a mediandiameter of 25 μm and a 90% particle size of 70 μm. TABLE 4 Metalelements Zn Fe Pb Cd Cu Content (wt %) 51.17 4.89 2.77 0.29 0.30

[0078] This zinc concentrate (280 g) and the iron-containing, acidicsolution (4.0 L) were fed into an autoclave having an internal capacityof 5 L and heated to 95° C. Thereafter, oxygen was blown directly intothe autoclave to build up a partial oxygen pressure of 0.8 MPa,whereupon the oxidizing and leaching reaction started. Twenty minuteslater, the autoclave was depressurized and the slurry was taken out it.The slurry was ground in the ball mill (for one pass over 5 minutes),turned back into the autoclave and subjected to another oxidizing andleaching reaction for 10 minutes in the same pressurized oxidizingatmosphere as created above. After this reaction, the autoclave wasdepressurized and the slurry was taken out of it and ground again in theball mill (for another pass over 5 minutes); after the grinding, theslurry was turned back into the autoclave and subjected to yet anotheroxidizing and leaching reaction for 10 minutes in the same pressurizedoxidizing atmosphere. After each of the leaching reactions in thepressurized atmosphere, a sample of the slurry was taken and filtered;the cake (residue) was washed thoroughly with water and the contents ofthe individual metals were measured. The percent zinc leach wasdetermined from the amounts of the initial zinc concentrate and theresidue, as well as the contents of their constituent metals.

[0079] The results are shown in Table 5, from which one can verify thatmore than 98% zinc leach was possible by leaching for a total period ofonly 40 minutes. TABLE 5 Cumulative pressurized Cumulative percent leachtime (min) zinc leach (%) 20 60.4 30 90.0 40 98.1

[0080] TABLE 6 Metal element Zn Fe Pb Cd Cu Content (wt %) 2.55 4.166.80 0.01 0.12

[0081] Using apparatus 21 to implement methods 11-20, one can improvethe rate of oxidation of ferrous ions in an iron-containing, acidicsolution by supplying oxygen into a pressurized atmosphere; in addition,the pressurized oxidation of the solution and the pressurized leachingof a zinc concentrate can be performed in one step, thereby shorteningthe leach time and streamlining the facilities to achieve substantialreduction in the overall cost.

[0082] Further according to the second and third aspects of theinvention, the slurry from the leaching step was subjected to thegrinding step with a grinding machine such as a ball mill to strip theelemental sulfur forming on the surfaces of the particles in the leachedzinc concentrate and thereafter the slurry was subjected to the sameleaching step; the leach time which was conventionally 6-10 hours couldbe reduced to less than a tenth. Thus, the overall reaction time wasconsiderably shorter than required in the prior art and substantial cutsin construction and operating costs were realized. As another advantage,methods 11-20 and apparatus 21 can be incorporated into the existingzinc refining process, enabling more zinc to be produced by smalladdition of equipment.

What is claimed is:
 1. An apparatus for leaching zinc concentrates whichcomprises: a pressure vessel for charging therein a solution containingat least free sulfuric acid and iron ions, a stirrer which is disposedin said pressure vessel, an oxygen gas supply pipe that extends intosaid pressure vessel from the outside of said pressure vessel, saidoxygen gas supply pipe having an oxygen gas inlet port which opens belowsaid stirrer, and a discharge pipe through which an iron-containing,acidic solution or a slurry that results from the reaction of saidsolution containing at least free sulfuric acid and iron ions isdischarged to the outside of the pressure vessel, said discharge pipehaving a drain port which is open in a lower part of said pressurevessel.
 2. The apparatus according to claim 1, wherein said pressurevessel is lined with titanium.
 3. The apparatus according to claim 1,which further comprises a charge pipe having an inlet port which opensin said vessel.
 4. The apparatus according to claim 1, wherein there isa first stirrer, a second stirrer and a third stirrer, said firststirrer, said second stirrer and said third stirrer being spaced apartwithin said pressure vessel.
 5. The apparatus according to claim 4,which further comprises a first partition which is disposed between saidfirst stirrer and said second stirrer; and a second partition disposedbetween said second stirrer and said third stirrer, to provide threecompartments within said pressure vessel.
 6. The apparatus according toclaim 5, which further comprises a charge pipe having an inlet portwhich opens in a lower part of a first compartment.
 7. The apparatusaccording to claim 5, wherein said first stirrer, said second stirrerand said third stirrer all have a plurality of blades.
 8. The apparatusaccording to claim 6, wherein said first stirrer, said second stirrerand said third stirrer all have a plurality of blades.